US3860492A - Liquid separation system - Google Patents

Liquid separation system Download PDF

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Publication number
US3860492A
US3860492A US37421173A US3860492A US 3860492 A US3860492 A US 3860492A US 37421173 A US37421173 A US 37421173A US 3860492 A US3860492 A US 3860492A
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condenser
liquid
section
netting
accordance
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Jr Alvin Lowi
Clifford C Wright
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Priority to DE19742459935 priority patent/DE2459935A1/de
Priority to NL7416639A priority patent/NL7416639A/xx
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/08—Thin film evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/007—Energy recuperation; Heat pumps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/343—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas
    • B01D3/346—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas the gas being used for removing vapours, e.g. transport gas
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/06—Flash evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/04—Aerobic processes using trickle filters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/10—Packings; Fillings; Grids
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/10—Packings; Fillings; Grids
    • C02F3/103—Textile-type packing
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S159/00—Concentrating evaporators
    • Y10S159/28—Porous member

Definitions

  • BOld 3/34, B01d 3/08 [58] Field of Search 159/1 W, 4 K, 13 B, 28 P, l59/DIG. 28, 8, 47 R, 24 A, 13 C; 202/236;
  • ABSTRACT A liquid separation purification system applicable to extracting purified liquids from or concentrating solids in a liquid feed material.
  • the system is particularly useful for extracting potable water from sea water. Cool feed liquid is pumped through the internal passages of a surface condenser section.
  • the feed liquid leaving the condenser section warmed by absorption of heat of condensation, is then further heated to a temperature below the boiling point of the liquid and then transferred to an absorption section.
  • the absorption section is formed of a matrix of material which divides the liquid into a plurality of thin films.
  • the condenser surface and absorber matrix are positioned in an insulated housing with openings between portions of the condenser and absorber.
  • a second noncondensing fluid (gas) circulating in the absorber is saturated with part of the heated liquid on the matrix.
  • the gas containing part of the feed fluid is circulated so that it travels toward the cooler condenser surface which strips the absorbedpart of the feed liquid from the gas and precipitates it into droplets and films to fall into a collection sump for the condensate.
  • the field of art to which the invention pertains includes the field of liquid purification systems, particularly with respect to extracting pure water from an aqueous feed liquid such as sea water.
  • the present invention overcomes the disadvantages of prior art liquid separation systems and operates with a minimum amount of input energy to purify feed liquid.
  • the system can be used where a small, efficient, portable purification system is required. Importantly, a single chamber can be utilized. The system does not require complex equipment and can be easily be expanded to increase output of purified liquid.
  • cooled feed fluid is pumped into a heat exchanger, e.g., a plurality of coils, of a condenser stage of the system.
  • the liquid is then transferred to a heating stage where it is heated and transferred to an evaporation stage consisting of a fixed bed absorption column.
  • a non-condensible gas is then utilized in a counterflow mode to absorb the volatile constituents in the feed fluid and transfer these vapors from the absorption column to the condenser stage where the vapors are condensed and collected for use.
  • FIG. 1 is a schematic illustration of the fluid purification system made in accordance with the principles of the invention
  • FIG. 2 is a sectional view illustrating the liquid distributor section utilized in the system of FIG. 1 taken along the line 22 of FIG. 1;
  • FIG. 3 is a sectional view of the liquid distributor section of FIG. 2 taken along the line 3-3 thereof;
  • FIG. 4 is a partial plan view of an exemplary absorbing curtain of monofilament Nylon fish net utilized in the system of FIG. 1;
  • FIG. 5 is a cross-sectional view illustrating the insulated chamber of the system of FIG. 1 taken along the line 55 thereof;
  • FIG. 6 is a graphicalrepresentation of the enthalpytemperature characteristics of a liquid purification system used to explain the effect of thermodynamic pinching
  • FIG. 7 is a graphical representation of the enthalpytemperature characteristics of a liquid purification system having an continuous bleed, semi-infinite stage transfer of a saturated gas from the evaporator section to the condenser section of the system;
  • FIG. 8 is a reproduction of a portion of the graph of FIG. 7, drawn to an enlarged scale.
  • Feed liquid such as sea water which is to be purified and concentrated in the system, travels through an inlet pipe 12 into a reservoir 14.
  • the inlet pipe 12 has a valve 16 (such as a float operated liquid level type) for regulat-. ing the amount of feed water to be fed into the system.
  • the reservoir 14 also contains a trap 18 and a blowdown valve 22 (which may be controlled by a salinity controller 23) for draining the sump.
  • the trap 18 is connected to the main portion of the reservoir 14 by means of a weir 2S.
  • Cooling coils 24 having an inlet 26 and an outlet 28 are positioned in the sump for cooling the residual liquid in the reservoir 14.
  • the cooled residual liquid recycled with the fresh raw feed fluid is pumped from the reservoir 14 into a pipe 30 by means of a pump 32.
  • the feed water then flows from the pump 32 into a pipe 36 and into a manifold 38 positioned on an insulated chamber 42 with side wall 43.
  • the central portion of the chamber 42 is divided by a transversely extending barrier wall 44 positioned in a plane parallel to the side wall 43 and contains a plurality of parallel connected condenser coils 46, on one side of the barrier wall 44, with water from themanifold 38,being distributed through the condenser coils.
  • the condenser coils may be formed of onequarter inch diameter coiled aluminum tubing.
  • the water in the condenser coils 46 is pumped from the lower level input of the manifold 38 to a second manifold 48 positioned on the side wall 43 of the insulated chamber positioned near the chamber top wall 54.
  • the manifold 48 joins the output ends of the condenser coils 46 and the water in the coils is then removed from the insulated chamber 42 and passed through a heat source 56 which heats the water to a temperature slightly below boiling, i.e. approximately F at sea level.
  • the heated water is then coupled from the heat source 56 to a third manifold 62 positioned on the side wall 64 of the insulated chamber 42 near the top wall 54.
  • the heated water at the manifold 62 is then distributed through a plurality of parallel pipes 66 and transferred from the pipes 66 by means of capillary action (as will be explained in greater detail hereinafter) to sheets of spaced-apart mono-filament Nylon fish netting 68.
  • the netting 68 hangs from just below the pipes 66 near the top of the chamber 42 and extends to a location in the chamber near the chamber bottom wall 72.
  • the barrier wall 44 divides the central third of the chamber 42 and terminates at top edge 78.
  • An opening 82 is defined by the edge 78 and the chamber top wall 54.
  • a branch wall 84 is formed at a downward acute angle with the barrier wall 44 from the edge 78 and extends downwardly toward the side wall 64 continuing as an interior bottom wall 86 spaced above the chamber bottom wall 72. The branch wall 84 causes the netting 68 to be bunched together near the evaporator sump 74.
  • Purified water which is formed in the chamber collects at the interior bottom wall 86 and is transferred by means of a pipe 92 which forms an opening 93 in the interior bottom wall 72 into a trap 94.
  • the trap 94 contains an opening 96 in the side wall thereof from which an outlet pipe 98 is used to drain off the purified water into a fresh water reservoir 100.
  • the side wall 43 of the insulated chamber 42 terminates below the manifold 38-and a curved side wall portion 102 extends outwardly and is curved and forms a continuation of the chamber bottom wall 72.
  • the interior bottom wall 86 is integral with an upward extension curved portion 104 parallelling the curved side wall portion 102 so that a fluid path 105 is defined between the interior bottom wall 86 and the chamber bottom wall 72 as well as the extension curved portion 104 and the side wall portion 102.
  • the interior bottom wall 86 and curved extension portion 104 defines a condenser sump 109 thereabove and below the condenser coil 46.
  • the extension curved portion 104 of the wall terminates at a baffle 106 which is spaced from thejunction of the side wall 43 and a horizontally formed wall 107 which interconnects with one end of the curved side wall portion 102 and the lower end of the chamber side wall 43.
  • a tangential blower 108 Spaced directly above the baffle 106 is a tangential blower 108 which causes air to flow from the bottom of the condenser coil 46 through the fluid path 105 in a direction shown by the arrows in FIG. 1 and upwardly into the chamber 42 past the netting 68. Note that the blower 108 can be omitted and natural circulation relied upon for the air flow; however, some reduc tion in performance can result.
  • the barrier 44 extends across the width of the chamber 42 so as to divide the chamber into a condenser cooling section 112 formed of the coils 46 and an absorption section 114 formed of the netting 68 as can be seen in FIG. 5.
  • the heated water which is transferred to the netting 68 travels downwardly along the netting as the fluid in the system, normally air, is passed through the path and upwardly between and through the netting 68.
  • the circulated air becomes saturated with the hot water vapor and travels so saturated through the opening 82 and into the cooling section 112.
  • the saturated air is cooled in the cooling section and fresh water is precipitated therefrom into the condenser sump 109 downwardly toward the interior bottom wall 86 whereupon it passes out through the pipe 92 into the trap 94.
  • the circulated air passes back through the cooling section 112 to the blower 108 where it is recirculated through the path 105.
  • air in place of air as a circulating medium, it should be understood that other gaseous fluids which will absorb water can be used in the system when the system is closed with respect to the gaseous material.
  • a plate with perforations or with horizontal (or vertical) slots, or a louvercd plate, or the like can interpose a plate with perforations or with horizontal (or vertical) slots, or a louvercd plate, or the like, depending upon the nature of the fixed bed material, particular parameters desired, type of condenser surface, all in furtherance of optimization of a particular system configuration.
  • the fluid path 105 can be blocked and the curved side wall portion 102 can be opened for exhaust to'the atmosphere by opening a first door 116 shown in dotted lines.
  • the door 116 is integrally formed with the wall portion 102 and a second door 118 in the lower portion of wall 64 can be opened (as shown in dotted lines) so that the blower 108 admits fresh air into the system at the bottom of absorption section 114.
  • the opening of the first door 116 and the second door 118 increases the heat rejection capacity of the system by admitting fresh air into the system.
  • the system can function satisfactorily to extract purified liquids without the use of a reservoir 14, cooling coils 24, a blowdown valve 22, a make-up valve 16 or a pump 32 with the inlet pipe connected directly to the manifold 38.
  • doors 116 and 118 as well as the pump 32 and the cooling coil 24 can be modulated to any degree separately or together to accomplish maximum performance for any combination of purified liquid extraction and feed fluid concentration.
  • multipass cross-counter flow can be obtained by reorienting the netting 68 perpendicular (edgewise) to the above mentioned slotted plate, and placing a multiplicity of horizontal baffles, slotted so as to mesh with the netting of curtains, to form a series of cross-baffles for guiding the vapor flow in a multipass cross-counter flow path through the netting without impeding the vertically falling liquid films.
  • Vapor bleed flow from the absorption section 114 to the condenser section 112 takes place via the slots in the vertical plate at selected locations where the interpass vertical portion of the vapor flow path is adjacent to the slotted plate.
  • FIG. 2 there is shown the interconnection between the manifold 62 and pipes 66 which transfer the heated water to the netting 68.
  • the pipes 66 are all connected in parallel in a plane parallel to the top wall 54 of the insulated housing. Openings 122 are formed at the lower surface of the pipes which enable water to leak out of the pipe and spray downwardly.
  • Capillary cloth 124 surrounds the outer surface of each pipe. The capillary cloth 124 saturates with water which is transferred to a flat portion 126 formed in a plane parallel to the pipes and directly therebelow.
  • wicking members 128 is illustrated positioned directly below the flat portion 126 and are formed in a plane parallel to the pipes 66 but extend transversely thereto.
  • the wicking members 128 are interspaced with a plurality of support rods 132 which extend in the plane of the wicking members.
  • The-wicking members 128 and support rods 132 are supported by means of a support plate 134 which contains a plurality of openings 136 directly below each of the support rods 132.
  • the exemplary embodiment of the netting 68 is formed of a monofilament Nylon fishnet of diamond-shaped configuration and is hung on support rods as a group of parallel curtains with each curtain extending through the opening 136 downwardly toward the reservoir 74 as illustrated in FIG. 1 in planes generally parallel to the condenser section.
  • the netting can be hung perpendicularly (edgewise) to the condenser section 112 (not shown).
  • the netting can be cut in the transverse direction and hung'as a multiplicity of coiled strands (not shown). In the latter two cases, the netting would not bow outwardly as in the arrangement of FIG. 1.
  • the netting 68 is knitted, containing no knots therein so as to enable the heated water to flow as a uniform film along each thread in every curtain toward the reservoir 74.
  • heated water is transferred from the pipe to the capillary cloth 124 and then to the wicking members 128 which in turn transfer the heated water to the netting.
  • the heated feed water flows into the flat portion 126 of the capillary cloth as the portion of the capillary cloth 124 surrounding the pipes 66 saturates.
  • the wicking members 128 are normally highly capillary and formed of a hydrophylic plastic fiber cord material which acts as a liquid conductor. Suitable for use as the Nylon fishnet is U.S. Net and- Twine material, Stock No. 4, having one inch stretch mesh, 144 meshes deep, and made of single knot (knitted) virgin monofilament Nylon material.
  • FIG. 5 there is shown a horizontal cross-sectional area of the chamber 42 taken along the line 5-5 of FIG. 1.
  • Each of the nets 66 extends across the width of the chamber.
  • additional netting material of wider width can be utilized.
  • additional coils 46 can be added in parallel should it be so desired.
  • thermodynamic processes involved in a water purification system can be described by means of an equilibrium line-operating line diagram which is plotted with the enthalpy (heat content) of a saturated mixture of air and water vapor as a function of temperature.
  • the equilibrium line illustrates the thermal energy content of moisture saturated air plotted against water temperature.
  • Two equilibrium lines are shown; the solid line illustrating the case where saturated air over pure water occurs in the condenser section, and the dotted line illustrating the case where saturated air over salt water exists in the evaporator section.
  • the operating lines depict energy balances between the water and air streams in the condenser section and the evaporator section.
  • the example uses a water flow rate three times that of the air flow rate in the system.
  • feed salt water enters the condenser coils at 60F (point 1 of FIG. 6) and exits the condenser coils at ll0F (point 2).
  • the water is then heated to lF (point 3) where it then enters the evaporator section.
  • the water leaves the evaporator section, it has cooled to a temperature of F (point 4).
  • Ratio of fresh product water to salt feed water 0.041; Number of effects 0.76
  • the number of effects is defined as the ratio of the energy required to boil a unit mass of pure water to steam at one atmosphere, starting with a liquid at 60F, to the energy required by the process to produce the same amount of pure water.
  • a solution to the pinch problem would be to start a very low ratio of liquid flow to air flow and gradually bleed air from the evaporator into the condenser. In this way, the operating line can be made to follow the equilibrium line without pinching occurring.
  • This solution requires careful control of the bleed air flow which is an advantageous feature of the effective water purification by means of the present system.
  • the performance of an eight stage design is substantially better than a single stage design described with respect to FIG. 6.
  • the product feed water ratio is 0.093 and the number of effects is 5.20.
  • 10.7 pounds of feed water is required, and 9.7 pounds of brine is rejected.
  • the corresponding thermal energy input would be 215 BTUs per pound of fresh water produced. A small additional amount of energy is required for pumping power.
  • the evaporator equilibrium line is lower (less energy per unit mass of dry air).
  • the water vapor pressure over the more concentrated feed fluid is less because of the presence of more dissolved solids in the fluid.
  • the operating lines will tend to separate requiring an increase in the heat input or increase in the evaporator size (number of transfer units) to maintain the same output.
  • a fundamental feature of muIti-stage water purification is the method of controlling the air bleed from the evaporator into the condenser by effecting a bleed differential between the top and bottom of an opening formed in a divider plate between the condenser and evaporator.
  • bleed flow control may be obtained with a slotted or perforated divider plate between the evaporator and the condenser.
  • Continuous staging where the operating lines are smooth curves that follow the equilibrium lines may be obtained by using a more compact packing at the face of the evaporator. In essence, the resistance to flow in the evaporator can be varied so that the desired bleed air flow control is inherently obtained.
  • the curtains of fishnet in the evaporator section are spaced closer together at the edge facing the condenser than in the center thereof so as to obtain a further regulation of the bleed flow.
  • FIG. 7 illustrates an equilibrium line operating line diagram for a continuous bleed, semi-infinite stage design.
  • this design which is illustrated in FIG. 1 is thermodynamically ideal.
  • the product water and condenser tube wall temperatures are also shown in FIG. 8, which is an enlarged view of one porition of FIG. 7.
  • the overall performance of the system operating at the conditions shown in FIG. 7 is a product to feed water ratio of 0.10 and a number of effects of 8.5. Greater concentration of the sea water feed and a higher product to feed water ratio can be achieved by recycling the concentrated brine (which lowers the evaporator equilibrium line, and separates further the operation lines) and by adding more thermal energy.
  • Carrier mediums other than air such as helium and hydrogen
  • Mixtures of helium and oxygen also have certain heat transfer and pumping power advantages. Pressure levels other than one atmosphere (both higher and lower) are permissable.
  • the magnitude of the pressure change within the unit is a function of the air flow rate, the temperature, the rate of phase change (evaporation and condensation), the rate of molecular weight change and the frictional and drag characteristics of the evaporator packing and condenser coils.
  • the bleed flow is proportional to:
  • m is the molecular weight of the air-water vapor mixture
  • AP is the pressure differential between the evaporator and the condenser
  • T is the temperature of the air-water vapor mixture at the location where bleed flow was taking place.
  • the exponent K is 0.5 for turbulent flow and 1.0 for laminar flow.
  • the bleed flow can be controlled either directly by using slotted or perforated plates or automatically by using variable packing in the evaporator section.
  • the oxygen in the fresh air could be utilized to bio-oxidize the organic components contained in the fluid being distilled.
  • the netting 68 can not only function as an absorption medium but also as a means for supporting a biological culture as well.
  • the netting can serve as a trickling filter medium allowing excess culture growth to slough off into the sump 14 through the pipe 76 connected to the evaporator sump 74 to be settled and separated as a solid.
  • the supernatant can be recycled into the system as usual.
  • any specially prepared cultures can be utilized to enhance the results of biooxidation.
  • a vapor staging distillation system for separating liquid from feed material, yielding a concentrate and a condensate comprising:
  • said divider wall having an opening in the top portion thereof appreciable vertical extent, said evaporator and condenser sections communicating directly through said opening whereby vapor from said films in said evaporation section is conveyed by said gas to said condenser section to effect a bleed differential between the top and bottom of said opening;
  • cooling means comprises a plurality of coils defining a flow path for said feed material.
  • said transferring means comprises a heat source for heating said feed material from said cooling means to a temperature near but below the boiling point of said liquid.
  • the means for providing thin films in said evaporator section includes flexible, vertically extending curtains of netting forming a fixed bed absorption column, said transferring means comprising means for feeding said feed material to the top of said netting to form said thin liquid films.
  • said means for feeding material comprises at least one horizontally extending conduit connected to a source of said feed material, said conduit defining openings therethrough, and including capillary means contiguous with said conduit openings and with the top of said netting whereby said feed material is conveyed from said conduit openings to said netting.

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  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
US37421173 1973-06-27 1973-06-27 Liquid separation system Expired - Lifetime US3860492A (en)

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US37421173 US3860492A (en) 1973-06-27 1973-06-27 Liquid separation system
DE19742459935 DE2459935A1 (de) 1973-06-27 1974-12-18 Anlage zur reinigung von fluessigkeit, insbesondere zur erzeugung von frischwasser aus meerwasser
NL7416639A NL7416639A (nl) 1973-06-27 1974-12-20 Installatie voor het afscheiden van vloeistoffen.

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Cited By (58)

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Publication number Priority date Publication date Assignee Title
US4243526A (en) * 1979-02-15 1981-01-06 Ransmark Sven Erik L Process for purifying liquids and a device for carrying out the process
US4261534A (en) * 1978-10-13 1981-04-14 Auro Roselli Inflated wing aircraft
US4276124A (en) * 1975-07-17 1981-06-30 Haakon Haakonsen Distillation system for sea water
WO1981003655A1 (en) * 1980-06-11 1981-12-24 Mitsubishi Electric Corp Apparatus for desalinizing brine
US4350570A (en) * 1979-09-17 1982-09-21 Maisotsenko Valery S Water desalination method
US4351651A (en) * 1980-12-12 1982-09-28 Courneya Calice G Apparatus for extracting potable water
FR2536738A1 (fr) * 1982-11-26 1984-06-01 Mitsubishi Electric Corp Appareil de dessalement
US4585523A (en) * 1984-02-27 1986-04-29 Giddings Edward H Vapor compression distillation apparatus
US4595459A (en) * 1982-11-12 1986-06-17 Mitsubishi Denki Kabushiki Kaisha Desalinization apparatus
US4687547A (en) * 1984-04-17 1987-08-18 Skw Trostberg Aktiengesellschaft Process for the separation of materials obtained by means of high pressure extraction
US4704189A (en) * 1982-03-12 1987-11-03 Geophysical Engineering Company Method of evaporating liquid from a solution
US4915792A (en) * 1987-02-11 1990-04-10 Sten Zeilon Process for separating a volatile component from a mixture
US4953694A (en) * 1985-12-18 1990-09-04 Hitachi, Ltd. Distilling apparatus
US4976824A (en) * 1988-06-16 1990-12-11 Naisin Lee Water distillation and aeration apparatus
WO1991009658A1 (en) * 1990-01-05 1991-07-11 T And G Technologies, Inc. Improved still and method
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US5535877A (en) * 1993-09-23 1996-07-16 Eastcott; Peter D. Glycol concentrator
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WO2001000533A1 (de) * 1999-06-25 2001-01-04 Alexander Von Poswik Verfahren und vorrichtung zum destillieren eines flüssigen stoffs aus einer lösung, insbesondere zur meerwasserentsalzung
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US20110056822A1 (en) * 2009-09-04 2011-03-10 Massachusetts Institute Of Technology Water Separation Under Reduced Pressure
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US8647477B2 (en) 2011-02-15 2014-02-11 Massachusetts Institute Of Technology High-efficiency thermal-energy-driven water purification system
WO2015055178A1 (de) * 2013-10-15 2015-04-23 WätaS Wärmetauscher Sachsen GmbH Reinigungsverfahren und reinigungsanlage für mit begleitstoffen belastetes wasser
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DE102014212973A1 (de) * 2014-07-03 2016-01-07 Siemens Aktiengesellschaft Verschaltungskonzept für eine thermische Aufbereitungsanlage
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US5082740A (en) * 1990-03-26 1992-01-21 The Dow Chemical Company Plastic clad metal laminate for heat transfer partitions
US5240560A (en) * 1990-08-06 1993-08-31 Gregory Marshall W Wastewater evaporator system
US5227027A (en) * 1990-08-23 1993-07-13 Topper Robert T High efficiency water distillation apparatus using a heat pump system and process for use thereof
US5535877A (en) * 1993-09-23 1996-07-16 Eastcott; Peter D. Glycol concentrator
WO2000020339A1 (de) * 1998-10-01 2000-04-13 Klaus Wolter Vorrichtung und verfahren zum gewinnen von nutzwasser aus rohwasser
WO2001000533A1 (de) * 1999-06-25 2001-01-04 Alexander Von Poswik Verfahren und vorrichtung zum destillieren eines flüssigen stoffs aus einer lösung, insbesondere zur meerwasserentsalzung
US20020166758A1 (en) * 2001-05-02 2002-11-14 Peter Vinz Evaporation process for producing high-quality drinking water and high-grade brine from any-grade salt water
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DE2459935A1 (de) 1976-07-01

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